Method for treatment of feedwaters by membrane separation under acidic conditions

ABSTRACT

A process for treatment of acidic waters via membrane separation equipment. A feedwater is maintained or adjusted to a pH of 4.3 or lower, and fed to a membrane separation system. In this manner, species such as total organic carbon (TOC) become more ionized, and (a) their rejection by the membrane separation process is significantly increased, and (b) their solubility in the reject stream from the membrane process is significantly increased. Passage of total organic carbon (TOC) through the membrane is significantly reduced. A recovery ratio at or exceeding eighty percent (80%) is achievable with most feedwaters, while simultaneously achieving a substantial reduction in cleaning frequency of the membrane separation equipment. The method is particularly useful for the preparation of high purity water.

RELATED PATENT APPLICATIONS

This patent application claims priority from and is a continuation of co-pending U.S. patent application Ser. No. 10/140,445, issued as U.S. Pat. No. 7,320,756, on Jan. 22, 2008; that application claimed priority from U.S. Provisional Patent Application Ser. No. 60/288,861, filed on May 5, 2001; each of those patent applications are incorporated herein by this reference in their entirety, including the specification, drawing figures, and claims.

TECHNICAL FIELD

This invention relates to a method for the treatment of acidic waters and wastewaters in membrane based water treatment, purification, and concentration systems, and to apparatus for carrying out the method. More particularly, the invention relates to methods for feedwater pretreatment and for operation of membrane based treatment systems such as reverse osmosis (“RO”) and nanofiltration (“NF”), which achieve increased solute rejection, thereby producing very high purity (low solute containing) product water, while significantly increasing on the on-stream availability of the water treatment equipment.

BACKGROUND

Naturally occurring acidic waters and acidic wastewaters from industrial processes are found in many geographical areas of the world. Conventional treatment methods commonly employed for treatment of such waters involve neutralization with alkali, to raise the pH, so that the water can be discharged or beneficially utilized. However, such methods are not always desirable, or even feasible in some instances, since such methods can add significant amounts of dissolved solids to the water. And, the cost of the necessary chemicals, and particularly the alkali, can be quite high.

If the treated water is to be utilized for potable applications, one commonly encountered standard which must be met is a World Health Organization criterion that potable water contain no more than 500 milligrams per liter of dissolved solids, and no more than 250 mg/l each of sulfate ion or chloride ion. However, criteria for reuse of water in most industrial applications are far stricter. Consequently, the common “straight neutralization” treatment process is not an acceptable option in a large number of water treatment applications.

In industrial applications, treatment/reclamation of acidic waters is most often presently based on ion-exchange or on reverse osmosis (RO) systems. Depending upon factors such as the level of hardness (polyvalent cations), total organic carbon (TOC), and other contaminants present in the water, anion-exchange can be used for treatment of such acidic feedwaters for the reduction/removal of acidity. Further, the addition of a cation exchange process before or after the anion exchange can indeed produce water that is almost completely demineralized. For this process, a weak base, an intermediate base, or a strong base anion exchange resin is employed, either singularly or in combination.

The major advantages of such prior art ion exchange treatment methods include the following:

(1) In industry, the method is considered “passive”, meaning that the process is not sensitive to changes in the influent characteristics.

(2) Compared to conventional reverse osmosis, the method has lower capital cost.

The major disadvantages of such prior art ion exchange treatment methods include the following:

(1) The quality, type (e.g., sodium based), and quantity of alkali needed (for regeneration of the IX resin) are actually higher and/or more restrictive than that required for straight neutralization, so the cost of the necessary chemicals is quite high.

(2) A very substantial volume of anion exchange resin is necessary; such resin is generally quite expensive. Thus, the initial and replacement cost of ion exchange resin in such systems is quite high compared to a membrane based treatment system.

(3) Depending upon the specific variety of ion exchange resin utilized, fouling by total organic carbon (TOC) can be quite high. Unfortunately, fouled anion resin can be difficult and expensive to clean. And, non-ionizable TOC components, such as IPA (iso-propyl alcohol) are not removed. Further, TOC components that are cationic in nature are not removed, either. Typically, removal of TOC, or at least significant reduction of TOC, is often an important requirement in a number of industrial applications where reuse of treated waters is desired.

In conventional membrane based systems that are used for treatment of acidic waste waters or of naturally acidic waters, the pH of the RO/NF feed is commonly adjusted by addition of alkali. Thus, such conventional RO/NF systems operate at, or reasonably close to, neutral pH conditions. With certain exceptions, conventional RO/NF systems are operated under such pH conditions in order to ensure that the RO/NF membranes are not damaged due to very high or to very low pH conditions. More fundamentally, for many commonly encountered membrane materials, the overall solute rejection across the membrane is typically highest at a pH of approximately 8. Thus, the conventional wisdom in the water treatment industry is to avoid operation of RO/NF membranes at low pH conditions.

Yet, some of the basic RO/NF process characteristics point to some particular potential advantages, when compared to ion exchange systems.

For example:

(1) RO/NF will simultaneously remove cationic as well as anionic species.

(2) RO/NF will, in general, remove a larger percentage of the TOC present before fouling of the media or membrane becomes a major concern. For instance, RO is capable of removing about eighty percent 80%, or sometimes more, of non-ionizable species, such as IPA.

(3) The capital, as well as the operating costs of RO/NF systems, unlike those of ion-exchange systems, are not particularly sensitive to the influent water chemistry characteristics.

Nonetheless, the conventional RO/NF systems known to me for treatment of such acidic waters, whether for wastewaters or for naturally occurring waters, still exhibit major shortcomings. Such deficiencies include:

(1) The quantity and cost of alkali needed to neutralize the RO feed remain comparable to mere neutralization, alone. Consequently, overall treatment costs are high, since RO system capital and operating costs must be added to the costs of neutralization.

(2) The combination of pH neutralization followed by RO is fundamentally inefficient, since the total dissolved solids content is first increased by the pH neutralization, but then the total dissolved solids content is decreased by the RO/NF process.

(3) RO/NF systems are quite susceptible to biofouling and/or particulate and/or organic fouling when they are operated at neutral or near neutral pH conditions. Unfortunately, however, the commonly utilized thin film composite membranes do not tolerate oxidizing biocides, such as chlorine. Consequently, control of biofouling is problematic, especially for treating waters containing organic contaminants.

Thus, a continuing demand exists for a simple, efficient and inexpensive process which can reliably treat acidic waters, whether naturally occurring or a wastewater from another process. It would be desirable to provide water of a desired purity, in equipment that requires a minimum of maintenance. In particular, it would be desirable to improve efficiency of feed water usage, and lower both operating costs and capital costs for water treatment systems, as is required in various industries, such as semiconductors, chemical production, mining, pharmaceuticals, biotechnology, and electric power plants.

Clearly, if a new water treatment process were developed and made available that combines the benefits of both conventional RO/NF membrane treatment and of ion exchange processes, particularly for the treatment of naturally occurring acidic waters as well as industrial waste waters, it would be of significant benefit. Additionally, such a process would be even more attractive if it were immune to the most vexing problems associated with either of reverse osmosis/nanofiltration or of ion exchange. In summary, an economically important new acidic water treatment process would necessarily offer some (if not most) of the benefits of both reverse osmosis and of ion exchange. At the same time, any such new process must be capable of effectively coping with the problems which beset the reverse osmosis/nanofiltration process or the ion exchange process.

OBJECTS, ADVANTAGES, AND NOVEL FEATURES

From the foregoing, it will be apparent that one important and primary object of the present invention resides in the provision of a novel method for treatment of water to reliably and continuously produce consistently pure water from acidic waters and wastewaters. More specifically, an important object of my invention is to provide a membrane based water treatment method which is capable of avoiding common pre-treatment costs and the operational fouling problems, so as to reliably provide a method of producing pure water while operating at high efficiency. Other important but more specific objects of the invention reside in the provision of a method for water treatment as described in the preceding paragraph which has the following attributes:

(1) on an overall “ownership and operating cost” basis, a process is provided which is cheaper to own and operate than conventional reverse osmosis/nanofiltration or ion exchange systems;

(2) it does not require “close control”, and accordingly it is easily able to cope with variability of feedwater;

(3) it is reliably capable of producing a consistently high quality product;

(4) the reverse osmosis or nanofiltration membranes may be arranged so as to render them unsusceptible to biological or organic fouling;

(5) that simultaneous removal of cationic, anionic, and non-ionic contaminants is achieved;

(6) that a very substantial portion of the TOC present be rejected or removed, independent of the ionic characteristics of the TOC components;

(7) that the addition of chemicals be minimized, not only as a matter of cost, but also as a matter of good environmental stewardship;

(8) that it can be practiced utilizing easily available components that are routinely manufactured by various companies;

(9) that available components are integrated synergistically, rather than in a contradictory manner, in order to provide the fullest possible benefit of available process equipment;

(10) that a high recovery rate, or volumetric efficiency, can be achieved when treating acidic waters and wastewaters;

(11) that a membrane can achieve a much higher productivity (flux) compared to conventional systems, and can do so while minimizing or eliminating membrane fouling; importantly, this also reduces capital and operating costs; and

(12) simplification and cost reduction in reverse osmosis or nanofiltration pre-treatment operations is attainable.

Other important objects, features, and additional advantages of my invention will become apparent to those skilled in the art from the foregoing, and from the detailed description which follows, and from the appended claims, in conjunction with the accompanying drawing.

BRIEF DESCRIPTION OF THE DRAWING

In order to enable the reader to attain a more complete appreciation of the invention, and of the novel features and the advantages thereof, attention is directed to the following detailed description when considered in connection with the accompanying drawings, wherein:

FIG. 1 illustrates a process flow diagram of the equipment utilized in a field test of my novel process for treating acid waters and wastewaters.

FIG. 2 illustrates a generalized process flow diagram for employing my novel water treatment process in a variety of applications and with a variety of feedwaters.

The foregoing figures, being merely exemplary, contain various unit processes or treatment elements that may be present or omitted from actual implementations depending upon the circumstances. An attempt has been made to draw the figures in a way that illustrates at least those elements that are significant for an understanding of the various embodiments and aspects of the invention. However, various other unit processes or treatment elements of an exemplary low pH membrane treatment process, especially as applied for different variations of the functional components illustrated, may be utilized in order to provide a complete water or wastewater treatment system suitable for use in a particular set of circumstances.

DETAILED DESCRIPTION

By means of extensive studies and the evaluation of the weaknesses of the existing processes, I have now developed a new water treatment process for the processing of acidic waters. Importantly, I have now confirmed that certain reverse osmosis/nanofiltration systems can be successfully operated at pH values as low as 2, often without any, or with minimal chemical or physical pretreatment. Currently, the lowest allowable pH limit is determined by the characteristics of commercially available reverse osmosis membranes, which is about a pH of 2.0, for continuous operation. In the future, if better (i.e., lower pH tolerant) membranes become available, my novel process will operate at even lower pH than the current limit of pH 2.0.

In spite of low pH operations, and contrary to conventional industry guidelines, extremely good rejection of cationic solutes, and of multivalent anionic solutes, is achieved. The rejection of sodium and ammonium ions is extraordinarily high, and this is a very significant and unexpected benefit from my new acidic water treatment process. The rejection of TOC is also very high under the process conditions of this new acidic water treatment process.

Also, I have found that the addition of a TOC removal process prior to feed of water to a low pH reverse osmosis membrane (or even after it, or even later after the anion exchange) can produce desired low TOC levels in the final product water. Acceptable TOC removal methods include:

(1) bubbling, including the use of microbubbles of air or an inert gas, in a storage tank or any other suitable column of water;

(2) mechanical or membrane treatment based degasification;

(3) ultraviolet radiation with 185 nm wavelength UV light, with or without the addition of oxidants such as hydrogen peroxide and/or ozone;

(4) addition of ferrous or ferric iron, along with hydrogen peroxide, if needed, for in-site formation of Fenton's reagent, which is known to be an effective oxidant for removing TOC compounds; or

(5) addition of ozone to feedwater, or to product water.

An especially important application is possible when the hydrogen peroxide present from semiconductor manufacturing wastewaters is augmented with ferrous or ferric salts. In such a case, the oxidation products are typically organic acids, and or carbon dioxide, which can be effectively removed by an anion exchange process. In contrast, IPA cannot be removed by the anion exchange, without prior oxidation, since it does not ionize.

Turning now to FIG. 1, the test setup for one evaluation of my treatment process for acidic wastewaters is shown. A three-stage reverse osmosis system was utilized. Feedwater having a conductivity of 2700 uS/cm was fed under pressure at 1.45 MPa at the rate of 2 m³/hr and at the pH of 2.6 and a temperature of 28 degrees C. to the first stage of the system. Subsequently, first stage reject was sent to the second stage at 1.4 MPa. Reject from the second stage was sent to the third stage at 1.35 MPa. Finally, rejected concentrate from the third stage was discharged at the pressure of 1.25 MPa and a pH of 2.4 at the rate of 0.5 m³/hr. The permeate from all three stages together was produced at the rate of 1.5 m³/h, a pressure of 0.3 MPa, and a conductivity of 28.5 uS/cm.

Overall, considering all three product stages, the product was produced at an average flux of 22.1 gallons per square foot per day (0.9 9089 m³/m2/day). This provided an overall recovery ratio of about 75%. The RO permeate was then sent to an anion exchanger at a pressure of 0.02 MPa, and produced a final effluent, after anion exchange, having a conductivity of 6.7 uS/cm.

The exemplary results of such testing, and in particular the very high purity of the RO product, as well as the quality of the final effluent from the anion exchange unit, demonstrate the efficacy of this novel process.

In FIG. 2, a generalized flow schematic is illustrated for use of my novel acidic wastewater treatment process in industry. Raw acidic water 10 is provided, either directly, as shown, to a low pH RO unit 12, or alternately, is routed through one or more pretreatment system components, as indicated in broken lines. First, the raw water 10 can be sent to a UV unit 20, in which preferably hydrogen peroxide 22 and/or a source of ferrous or ferric iron 24 is provided. Then, the partially treated water is routed to a degas 30 or other liquid-gas contactor, for further removal of total organic carbon (TOC) constituents. Reject from the RO is sent for further treatment or discharge as appropriate. Permeate as indicated by line 32 is sent to an anion ion exchange (“I-X”) unit 34. Then, the product from the ion exchange treatment is ready for use as makeup to an ultrapure water system 40, or alternately, can be sent to primary mixed bed I-X units 42 and/or secondary mixed bed I-X units 44. Then, the high purity water can be used, or further treated as appropriate, such as in a filter unit 50 or a second UV treatment apparatus 52, before being sent to an ultrapure water (UPW) system 54.

The process described herein can be practiced in membrane separation equipment which includes at least one separation unit having a membrane separator, to produce a low solute containing product stream and a high solute containing reject stream. In the process, a feedwater stream containing solutes therein is provided for processing. In some cases, the solutes may include at least one constituent that contributes to membrane fouling when the feedwater does not contain free mineral acidity. Before processing the feedwater in a membrane separator, the pH of the feedwater is adjusted, if necessary, to assure that at least some free mineral acidity is present in the feedwater as input to the membrane separator. The pH adjusted feedwater is fed through the membrane separation equipment, in which the membrane substantially resists passage of at least some dissolved species therethrough, to concentrate the feedwater to a preselected concentration factor, to produce (i) a high solute containing reject stream, and (ii) a low solute containing product stream. Often, in this process, the pH of the feedwater is adjusted to a pH of about 4.3 or lower. Importantly, the process can be applied in applications where the membrane separator is a reverse osmosis membrane, or a nanofiltration membrane, or a loose reverse osmosis membrane.

For many important applications, the feedwater includes one or more total organic carbon (TOC) constituent(s), and the total organic carbon (TOC) constituent(s) are effectively removed from the product stream. For many applications, treatment objectives include removal of the TOC so that the TOC present in the product stream is approximately ten percent (10%) or less of the concentration of such constituent(s) in the feedwater. The process can be advantageously utilized when the TOC components include one or more substantially non-ionizable species, such as isopropyl alcohol, and acetone.

Other constituent removals are also of importance. For example, when the feedwater includes sodium ions, treatment in some applications be can be achieved to the degree where the product stream contains approximately two percent (2%) or less of the sodium ion concentration present in the feedwater. And, when the feedwater includes ammonium ions, treatment in some applications can be achieved to the degree where the product stream contains approximately eight percent (8%) or less of the ammonium ion concentration present in the feedwater. Where the feedwater includes chloride ions, treatment in some applications can be achieved to the degree that the product stream contains approximately twenty-five percent (25%) or less of the chloride ion concentration present in the feedwater. Where sulfate ions are present in the feedwater, treatment can be achieved to the degree that the product stream contains approximately one-half of one percent (0.5%) or less of the sulfate ion concentration present in the feedwater. However, with fluoride ions, it is common that the concentration of fluoride ions present in the product stream is approximately the same as the concentration of fluoride ions present in the feedwater stream.

As an additional pretreatment process in the treatment of a feedwater at low pH in a membrane separation system, the free mineral acidity present in the product stream can be removed, at least to some desirable degree, if not substantially completely, by treatment in an anion exchange system. An appropriate anion exchange system could be (a) a weak base anion exchange system, (b) an intermediate base anion exchange system, or (c) a strong base anion exchange system. If desired, the anion exchange system can be set up to process the product stream to effectively removes all anions contained therein.

For further treatment effectiveness, particularly for removal of TOC, an additional feedwater treatment, prior to treatment in the membrane separation unit, can be added. On suitable such additional treatment process includes the addition of either ferrous or ferric ions to the feedwater. In addition, in such a process, hydrogen peroxide could be further added, for example to create a Fenton's reagent for treatment of total organic carbon (TOC). In this manner, total organic carbon constituents can be effectively eliminated in the product stream. Alternately, or additionally, the feedwater stream can be further treated prior to membrane separation by adding of irradiation of the feedwater stream with a UV light source, and in such a manner, the total organic carbon constituents can be effectively eliminated from the product stream. For yet further treatment to achieve high purity water effluent from the overall treatment process, the additional process of irradiation of the product water stream with a UV light source, so that the total organic carbon constituent(s) is effectively eliminated from the product stream.

In yet another embodiment, the process further includes ozonation of the feedwater stream with an ozone containing gas, and wherein the total organic carbon constituents are effectively eliminated from the product stream. Alternately, or additionally, the process can further include ozonation of the product water stream with an ozone containing gas, so that the total organic carbon constituent(s) is effectively eliminated from the product stream.

In yet another embodiment of the process of treating a feedwater in low pH membrane separation operation, in those cases where the feedwater contains hydrogen peroxide, either from an industrial process or via a prior treatment, the process can be set up to further include pretreatment of the feedwater stream in an activated carbon system, so that the hydrogen peroxide is effectively eliminated from the product stream.

Production of permeate product water at a production rate (flux) of at least 15 gallons per square foot per day is normally easily achievable. Importantly, the recovery is normally at least sufficient so that the ratio of the quantity of the product stream produced to the quantity of the feedwater stream provided is about seventy-five percent (75%) or more. In other embodiments, the recovery is sufficient so that the ratio of the quantity of the product stream produced to the quantity of the feedwater stream provided is about eighty percent (80%) or more. In yet other embodiments, the recovery is sufficient so that the ratio of the quantity of the product stream produced to the quantity of the feedwater stream provided is about eighty-five percent (85%) or more. In still further embodiments, the recovery is sufficient so that the ratio of the quantity of the product stream produced to the quantity of the feedwater stream provided is about ninety percent (90%) or more. In certain applications, it is anticipated that the recovery will be sufficient so that the ratio of the quantity of the product stream produced to the quantity of the feedwater stream provided is about ninety five percent (95%) or more.

For still more treatment in combination with the basic low pH membrane separation process described herein, other pretreatment processes may be provided prior to acidification of the feedwater. Such pretreatment processes can include (a) media filtration, (b) cartridge filtration, (c) ultrafiltration, (d) nanofiltration, (e) oxidant removal, (f) softening, (g) cation exchange, (h) degasification, or (i) oxygen removal. In some embodiments, pretreatment using cation exchange is accomplished by weak acid cation exchange. In other embodiments, the pretreatment using cation exchange is accomplished by the use of strong acid cation exchange. Also, the pretreatment process of oxidant removal can include the addition of sodium meta-bisulfite to the feedwater.

More generally, the process provided herein can be fundamentally described as the treatment of a feedwater stream in membrane separation equipment, wherein the membrane separation equipment has at least one unit having a membrane separator, to produce a low solute containing product stream and a high solute containing reject stream. In the process, a feedwater stream containing solutes therein is provided, and the pH of the feedwater stream is adjusted, if necessary, to assure at least some free mineral acidity presence, to produce a pretreated feedwater stream. The pretreated feedwater stream, having a preselected pH, is passed through the membrane separation equipment, wherein the membrane substantially resists the passage of at least some dissolved species therethrough, to concentrate the pretreated feedwater to a preselected concentration factor. A high solute containing reject stream having a pH lower than the pretreated feedwater stream is produced. Also, a low solute containing product stream having a pH higher than the pretreated feedwater stream is produced.

The unique process disclosed herein can also be advantageously practiced by further including the process of utilizing the reject stream from the membrane separation process in the regeneration of a cation exchange system. For example, such a process could include utilizing the reject stream as an acid source for regeneration of a weak acid cation exchange system. Or, such a process could include utilization of the reject stream as an acid source for regeneration of the strong acid cation exchange system.

The method and apparatus for processing acidic waters via membrane separation equipment, and in particular, via the combination of reverse osmosis/nanofiltration and ion exchange equipment, by the process design as described herein, provides a revolutionary, paradoxical result, namely, simultaneous decrease in total dissolved solids in the water to be treated, and reliable, high purity in the purified RO permeate. This method of operating membrane separation systems, and in particular, for operating reverse osmosis systems, represents a significant option for treating acidic waters, while simultaneously reducing capital and operating costs of the water treatment system. Further, given the efficiencies, dramatically less usage of chemical reagents, whether for neutralization, or for ion exchange regenerant or for RO cleaning, will be achieved per gallon of product water produced.

It will thus be seen that the objects set forth above, including those made apparent from the proceeding description, are efficiently attained, and, since certain changes may be made in carrying out the above method and in construction of a suitable apparatus in which to practice the method and in which to produce the desired product as set forth herein, it is to be understood that the invention may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. For example, while I have set forth an exemplary design for treatment of acidic waters, other embodiments are also feasible to attain the result of the principles of the method disclosed herein. Therefore, it will be understood that the foregoing description of representative embodiments of the invention have been presented only for purposes of illustration and for providing an understanding of the invention, and it is not intended to be exhaustive or restrictive, or to limit the invention to the precise forms disclosed. On the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as expressed in the appended claims. As such, the claims are intended to cover the methods and structures described therein, and not only the equivalents or structural equivalents thereof, but also equivalent structures or methods. Thus, the scope of the invention, as indicated by the appended claims, is intended to include variations from the embodiments provided which are nevertheless described by the broad meaning and range properly afforded to the language of the claims, or to the equivalents thereof. 

1. A process for treatment of a feedwater stream using reverse osmosis membrane separation equipment, said reverse osmosis membrane separation equipment comprising at least one reverse osmosis membrane separator, to produce a low solute containing product stream and a high solute containing reject stream, said process comprising: (a) providing a feedwater stream containing solutes, said solutes comprising at least one constituent that can contribute to fouling of said reverse osmosis membrane separator in the absence of free mineral acidity; (b) pretreating said feedwater stream by controlling the pH of said feedwater stream to about 4.3 or lower by the time said feedwater stream enters said reverse osmosis membrane separator, to assure at least some free mineral acidity in the pretreated feedwater; (c) passing the resultant pretreated feedwater stream through said reverse osmosis membrane separation equipment, said reverse osmosis membrane separation equipment substantially resisting passage of at least some dissolved species therethrough, to concentrate said pretreated feedwater to said preselected concentration factor, to produce (i) a high solute containing reject stream, and (ii) a low solute containing product stream; (d) wherein feedwater stream comprises one or more total organic carbon (TOC) constituents, and wherein said one or more total organic carbon (TOC) constituents are substantially prevented from passing through said reverse osmosis membrane separator to said product stream; and (e) wherein said one or more total organic carbon (TOC) constituents comprise one or more non-ionizable species, said one or more non-ionizable species comprising isopropyl alcohol, or acetone.
 2. The process as set forth in claim 1, wherein said total organic carbon (TOC) constituents in said product stream is approximately ten percent (10%) or less of the concentration of such total organic carbon (TOC) constituents in said feedwater stream.
 3. The process as set forth in claim 1, or in claim 2, wherein said feedwater stream comprises ammonium ions, and wherein said product stream contains approximately eight percent (8%) or less of the ammonium ion concentration present in said feedwater stream.
 4. The process as set forth in claim 1, or in claim 2, further comprising (i) adding either ferrous or ferric ions to said feedwater stream before entry of said feedwater stream to said reverse osmosis membrane separation equipment, as reactants to facilitate removal of total organic carbon (TOC) constituents, and (ii) adding hydrogen peroxide to said feedwater stream at any point before feed to said reverse osmosis membrane separation equipment.
 5. The process as set forth in claim 1, or in claim 2, further comprising ozonation of said feedwater stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively prevented from entering said product stream.
 6. The process as set forth in claim 1, or in claim 2, further comprising ozonation of said product water stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively eliminated from said product stream.
 7. The process as set forth in claim 1, or in claim 2, further comprising removal of oxidants from said feedwater stream, and wherein said pretreatment process of oxidant removal comprises the addition of sodium meta-bisulfite to said feedwater stream.
 8. The process as set forth in claim 7, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, or (v) degasification.
 9. The process as set forth in claim 1, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, (v) degasification, or (vi) oxygen removal.
 10. The process as set forth in claim 1, wherein said membrane separator comprises a loose reverse osmosis membrane.
 11. A process for treatment of a feedwater stream using reverse osmosis membrane separation equipment, said reverse osmosis membrane separation equipment comprising at least one reverse osmosis membrane separator, to produce a low solute containing product stream and a high solute containing reject stream, said process comprising: (a) providing a feedwater stream containing solutes, said solutes comprising at least one constituent that can contribute to fouling of said reverse osmosis membrane separator in the absence of free mineral acidity; (b) pretreating said feedwater stream to reduce the pH of said feedwater stream to about 4.3 or lower by the time said feedwater stream enters said reverse osmosis membrane separator, to assure at least some free mineral acidity in the pretreated feedwater; (c) passing the resultant pretreated feedwater stream through said reverse osmosis membrane separation equipment, said reverse osmosis membrane separation equipment substantially resisting passage of at least some dissolved species therethrough, to concentrate said pretreated feedwater to said preselected concentration factor, to produce (i) a high solute containing reject stream, and (ii) a low solute containing product stream; (d) wherein feedwater stream comprises one or more total organic carbon (TOC) constituents, and wherein said one or more total organic carbon (TOC) constituents are substantially prevented from passing through said reverse osmosis membrane separator to said product stream; and (e) wherein the ratio of the quantity of said product stream produced to the quantity of said feedwater stream provided is about eighty percent (80%) or more.
 12. The process as set forth in claim 11, wherein the ratio of the quantity of said product stream produced to the quantity of said feedwater stream provided is about eighty-five percent (85%) or more.
 13. The process as set forth in claim 11, wherein the ratio of the quantity of said product stream produced to the quantity of said feedwater stream provided is about ninety percent (90%) or more.
 14. The process as set forth in claim 11, or in claim 12, or in claim 13, wherein said total organic carbon (TOC) constituents in said product stream is approximately ten percent (10%) or less of the concentration of such total organic carbon (TOC) constituents in said feedwater stream.
 15. The process as set forth in claim 14, wherein said feedwater stream comprises ammonium ions, and wherein said product stream contains approximately eight percent (8%) or less of the ammonium ion concentration present in said feedwater stream.
 16. The process as set forth in claim 11, or in claim 12, or in claim 13, wherein said feedwater stream comprises ammonium ions, and wherein said product stream contains approximately eight percent (8%) or less of the ammonium ion concentration present in said feedwater stream.
 17. The process as set forth in claim 14, further comprising (i) adding either ferrous or ferric ions to said feedwater stream before entry of said feedwater stream to said reverse osmosis membrane separation equipment, as reactants to facilitate removal of total organic carbon (TOC) constituents, and (ii) adding hydrogen peroxide to said feedwater stream at any point before feed to said reverse osmosis membrane separation equipment.
 18. The process as set forth in claim 11, further comprising ozonation of said feedwater stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively prevented from entering said product stream.
 19. The process as set forth in claim 11, further comprising ozonation of said product water stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively eliminated from said product stream.
 20. The process as set forth in claim 11, further comprising pretreatment for removal of oxidants from said feedwater stream, and wherein said pretreatment process of oxidant removal comprises the addition of sodium meta-bisulfite to said feedwater stream.
 21. The process as set forth in claim 20, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, or (v) degasification.
 22. The process as set forth in claim 11, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, (v) degasification, or (vi) oxygen removal.
 23. The process as set forth in claim 11, wherein said membrane separator comprises a loose reverse osmosis membrane.
 24. A process for treatment of a feedwater stream using membrane separation equipment, said membrane separation equipment comprising at least one membrane separator, to produce a low solute containing product stream and a high solute containing reject stream, said process comprising: (a) providing an acidic feedwater stream containing solutes, said acidic feedwater stream having a pH that assures the presence of free mineral acidity therein; (b) pretreating said acidic feedwater stream, if necessary, to maintain the acidity of said feedwater stream to a pH of between about 4.3 and about 2.0 at the time said feedwater stream enters said membrane separator, to assure at least some free mineral acidity remains in the pretreated feedwater; (c) passing the resultant pretreated feedwater stream through said reverse osmosis membrane separation equipment, said membrane separation equipment substantially resisting passage of at least some dissolved species therethrough, to concentrate said pretreated feedwater to said preselected concentration factor, to produce (i) a high solute containing reject stream, and (ii) a low solute containing product stream;
 25. The process as set forth in claim 24, wherein said membrane separator comprises a reverse osmosis membrane separator.
 26. The process as set forth in claim 24, wherein said membrane separator comprises a loose reverse osmosis separator.
 27. The process as set forth in claim 24, wherein said membrane separator comprises a nanofiltration separator.
 28. The process as set forth in claim 24, wherein in the pH of said acidic feedwater stream is adjusted to a pH of about 2.6 or lower.
 29. The process as set forth in claim 24, wherein said acidic feedwater stream comprises total organic carbon (TOC) constituents, and wherein said total organic carbon (TOC) constituents are substantially prevented from entering said product stream.
 30. The process as set forth in claim 29, wherein said total organic carbon (TOC) constituents in said product stream are approximately ten percent (10%) or less of the concentration of such constituents in said acidic feedwater stream.
 31. The process as set forth in claim 24, wherein said acidic feedwater stream comprises sodium ions, and wherein said product stream contains approximately two percent (2%) or less of the sodium ion concentration present in said feedwater stream.
 32. The process as set forth in claim 24, wherein said acidic feedwater stream comprises ammonium ions, and wherein said product stream contains approximately eight percent (8%) or less of the ammonium ion concentration present in said acidic feedwater stream.
 33. The process as set forth in claim 24, wherein said acidic feedwater stream comprises chloride ions, and wherein said product stream contains approximately twenty five percent (25%) or less of the chloride ion concentration present in said acidic feedwater stream.
 34. The process as set forth in claim 1, or in claim 11, or in claim 24, further comprising treating said product stream in an anion exchange system, said anion exchange system removing free mineral acidity from said product stream.
 35. The process as set forth in claim 34, wherein said anion exchange system is selected as one or more system from the group consisting of (a) a weak base anion exchange system, (b) an intermediate base anion exchange system, and (c) a strong base anion exchange system.
 36. The process as set forth in claim 34, wherein said anion exchange system effectively removes all anions contained in said product stream.
 37. The process as set forth in claim 24, wherein said pretreatment comprises adding ferric or ferrous ions to said acidic feedwater stream.
 38. The process as set forth in claim 37, further comprising adding hydrogen peroxide to said acidic feedwater stream.
 39. The process as set forth in claim 24, wherein said pretreatment comprises use of cation exchange.
 40. The process as set forth in claim 39, wherein said pretreatment using cation exchange comprises use of weak acid cation exchange.
 41. The process as set forth in claim 39, wherein said pretreatment using cation exchange comprises use of strong acid cation exchange.
 42. The process as set forth in claim 27, wherein said pretreatment comprises irradiation of said acidic feedwater stream with a UV light source, and wherein said total organic carbon constituents are effectively eliminated from said product stream.
 43. The process as set forth in claim 29, further comprising irradiation of said product stream with a UV light source, and wherein said total organic carbon constituents are effectively eliminated from said product stream.
 44. The process as set forth in claim 24, wherein said pretreatment process comprises oxidant removal, said oxidant removal comprising the addition of sodium meta-bisulfite to said feedwater stream.
 45. The process as set forth in claim 24, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, or (v) degasification.
 46. The process as set forth in claim 24, further comprising one or more additional pretreatment processes, said additional pretreatment processes comprising (i) media filtration, (ii) cartridge filtration, (iii) ultrafiltration, (iv) nanofiltration, (v) degasification, or (vi) oxygen removal.
 47. The process as set forth in claim 24, wherein said acidic feedwater stream comprises hydrogen peroxide, and wherein said process further comprises treatment of said acidic feedwater stream in an activated carbon system, so as to effective remove hydrogen peroxide from said acidic feedwater stream.
 48. The process as set forth in claim 24, further comprising ozonation of said feedwater stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively prevented from entering said product stream.
 49. The process as set forth in claim 24, further comprising ozonation of said product water stream with an ozone containing gas, and wherein said total organic carbon (TOC) constituents are effectively eliminated from said product stream. 